Sampling and metering device for fluent solid materials



May 27, 1958 s. E. SHIELDS ETAL 2,836,069

SAMPLING AND METERING DEVICE FOR FLUENT SOLID MATERIALS Filed Sept. 1, 1955 5 Sheets-Sheet 1 Air 0 Supply 00 RECORDER FIG. 1

VIBRATOR mvemoas: g Hd/dONVlS 8 Sfanley E. Shield:

-Pln'lip W. Dewey William A. Shire, Jr.

ATTORNEY y 7, 1958 s. E. SHIELDS ETAL 2,836,069

SAMPLING AND METERING DEVICE FOR FLUENT SOLID MATERIALS Filed Sept. 1, 1955 5 Sheets-Sheet 2 INVENTORS: Stanley E. .Sliie/ds Philip M! Dewey William A. S/u're, Jr.

W z'mavnem ATTORNEY s. E. SHIELDS ET AL SAMPLING AND METERING DEVICE FOR .FLUENT soup MATERIALS Filed Sept. 1. 1955 5 Sheets-Sheet 3 FIG. 60

FIG. 8

INVENTORS: Stanley E. Shields Philip W. Dewey BY William A. Shire, Jr. g m" 0.9M

FIG.

ATTORNEY y 1958 s. E. SHIELDS ET AL 2,836,069

SAMPLING AND METERING DEVICE FOR FLUENT SOLID MATERIALS Filed Sept. 1. 1955 5 Sheets-Sheet 4 m mHE QOIBZOQ msmt.

.. f Y m J, M m Ns s O/T E T V a A N W w m w flm Y B SAMPLING AND METERING DEVICE FOR FLUENT SOLID MATERIALS Filed Sept. 1, 1955 May 27, 1958 s. E. SHIELDS ET AL 5 Sheets-Sheet 5 INVENTORS: Stanley E. Shields Phil/)0 h. Dewey William A. Shire, Jr.

ATTORNEY United States Patent SAWLING AND METERING DEVICE Eon FLUENT soLm MATERIALS Application September 1, 1955, Serial No. 532,073

6 Claims. (Cl. 73-424) This invention relates to an improved method and apparatus for continuous sampling of flowing granular materials. It further pertains; to the sampling of fluent solids and analysis thereof for components thereof. It has particular reference to a method and apparatus for measuring continuously the concentration of deposits, such as carbon, on circulating fluid solid catalysts.

in a number of hydrocarbon conversion processes employing finely divided solid catalysts, there is a deposition of carbon or carbonaceous coatings. In regenerating such catalyst material, it is desired to control the regeneration operation in terms of the proportion of carbon on the catalyst. Ordinarily such regeneration may be effected by burning the deposits from the contact material by means of an oxygen-containing gas. To have an eflicient regeneration, it is essential that the rate of burning and proportion of oxygen be controlled. Likewise the deposition of carbonaceous deposits on finely divided contacting materials during a reaction or conversion is indicative of the reaction condition. These conditions may be altered from time to time in accordance wth the extent of carbonaceous deposit.

As is well known, the carbon on catalyst can be deermined by withdrawing a batch sample from a catalyst mass and thereafter measuring the proportion of carbon. This may be done by conventional test procedures involving the burning of the carbonaceous deposit from the solids and analyzing the combustion gases for CO In the usual case Where random samples are drawn by operators that are delivered to a technical service laboratory and there measured, the total elapsed time from the drawing of the sample to the reporting back by the laboratory may be several hours. Obviously where large quantifies of catalyst materials are being handled, the difference between the control based on information on a continuous sample and that based on information which is several hours late and on random samples is satisfactory neither from the reliability of the test nor the sensitivity of the control operation.

Batch random sampling provides only sutficient data to indicate that an accurately controlled and continuous sampling system would be very useful. An important object is therefore to provide a sampling device for th withdrawal of a uniform increment of finely divided solids from a flowing mass of such solids. A further object of the invention is to provide a fully automatic system for continuously sampling solids from a standpipe and giving a prompt analysis so as to permit process control. A more specific object of this invention is to provide a sampling apparatus useful in a continuous operating system which will give accurate carbon-on-catalyst readings and which is compartively simple in the method of operation as well as in the elements of construction. These and other objects of the invention will become apparent as the more detailed description thereof proceeds.

Briefly the operation of our analyzer is based on the withdrawal of a catalyst sample continuously, precisely metering a portion of the withdrawn sample, removing any deposit from the metered sample by combustion, and measuring the products derived from such combustion. All of these operations are performed in a continuous and automatic manner. The combustion technique of determining carbon deposits on the metered sample of catalyst has been adopted since it aflords data of a more precise and reliable quality than is obtainable by variation in such properties of the metered spent catalyst as color, electrical resistivity, density or the like. The invention will be more fully understood from the following detailed description read in conjunction with the accompanying drawings which form a part of the specification and in which:

Figure 1 is a schematic flow diagram of our improved carbon-on-catalyst analyzer system;

Figure 2 is an elevation of the solids sampling and metering apparatus;

Figure 3 is a top View of the apparatus in Figure 2;

Figure 4 is an elevation, partly in section, of the device in Figure 2;

Figure 5 is a view taken along the line 5-5 in Figure Figures 6 and 6a are detailed views of the catalyst nozzle and diverting shield;

Figures 7 and 8 are views of the sample wheel and sample Wheel scraper;

Figure 9 is a schematic view of the furnace and control included in the analyzer assembly of Figure 1;

'Figure 10 is a cross section taken along the line 1010 in Figure 9; and

Figure 11 is an enlarged elevation, partly in section, of the catalyst take-01f tube.

Referring to Figure 1, the spent catalyst sample taken from the catalyst standpipe 10 issues from the catalyst delivery tube 11 into the catalyst metering assembly 12. The metered sample of catalyst from 12 is introduced by conduit 13 into the furnace 14 wherein the deposit on the catalyst is burned by an oxidizing gas. When oxygen is used it is metered into the furnace 14 from a supply via line 15 at a rate of 10 to 15 times that required to complete combustion of the carbon on the catalyst. A capillary-type flow meter 16 has been found particularly suitable for the metering of the oxygen. To insure constancy of the oxygen supply pressure at the inlet to the flow meter 16, we provide two pressure-reducing regulators in series. The usual type of cylinder pressure regulator is used for initial pressure reduction and the second pressure regulator 17 further reduces the oxygen pressure to that which gives the desired oxygen flow with the particular capillary-type flow meter 16 employed.

In a commercial installation the use of air as the oxidizing gas is preferred, since it avoids the encumbrances of cylinder oxygen. However, when air is used a higher temperature is required in the furnace 14 for an equivalent amount of carbon removal. For example, with a synthetic silica-alumina cracking catalyst having 0.87 percent carbon, a furnace temperature of MOO-1150" F. will give a carbon-free catalyst, whereas with air as the oxidizing gas a temperature of 1250l300 F. is required for comparable carbon removal. In using air, the oxygen metering set-up can be eliminated since the air comes in directly with the catalyst from the metering assembly housing 12. However, the oxygen injection points can also be left open to draw in air from the surrounding atmosphere by means of the aspirator set-up.

The oxidizing gas, whether air or oxygen, and the cata lyst flow concurrently down through the furnace 14. It has been found that installing the furnace tube 14 at an angle of about 30 with the horizontal is conducive to good catalyst flow. To further insure continuity of the catalyst flow, the furnace 14 is vibrated lightly by means a frequency of 60 cycles per second.

gas in cell 27;.

per unit time.

' of a vibrator 18 such as a Syntron vibrator operating at The regenerated catalyst. from the outlet 19 of the .furnace-l i is collected in a receiver 20 attached by a i coupling 21 for rapiddisengagement; A gate valve .iS provided between the .receiverlt); and .the furnace 14 to permit operation while the receiver .20 is being emptied.

'- The"eflluent combustion gasfrom the furnace 14. flows successively via line .23 through a water trap 24, .a drier tube 125;.andaHopcalite tube 26 before entering the i CO meter and recorder 27. Any CO in the combustion 5 gas should be converted to CO before introduction into I the meter 27, and the Hopcal'ite tube 26 is provided for this purpose. This insures measurement of ,all thecatalyst carbon'burned therefromainthe furnace .14 by the i oxidizing gas. A' thermal conductivity type meter 27 5' can banned for measuringthe CO content of the comanemone 7 1 analyzed is relatively small and discarded, higher tem- 'peratu'res above about 1100 F.1l50 F. can be'used with air as the oxidizing gas. In anyevent, the tem perature of the furnace 14 is controlled. at. the desired level by temperature-control means 33 as will be described below.

Referring to Figures 2 to 8, and ll, thesampling and metering assembly 12 includes a casing 34 from which the delivery tube 11 extends through the'wall of the standpipe 10 Preferably, the tube 11 is horizontal or sloped downwardly.-

In Figure ll, we have shown details of a preferred means for introducing the sample tube 11 into the stand bustion gas. Toinsure.dependablepertormance ofthis type .of CO meter, the combustijon gas should be m'ois ture freeand water trap 24 and driertube 25 fireprovided for this purpose.

7 Theggasesissuing from .the COconverter tube 25 enter' the measuring cell 27m of the CO meter ,27 where the Q0 ;content is measuredwith reference to a standard This may be the gases under test from.

which CO has been removed by means of adsorber 27a containing an adsorbent such as soda lime; The CO 'free stream passes from the adsorber'27n and enters the" reference cell 271'. -Alternatively, the reference cell 27r may contain asealed quantity of an appropriate reference gas which may be of background composition,"i. e; a 7

sample of combustion gas minusCO or pure In that event the adsorber 27a is omitted and thecombustion gases pass directly from cell 27m to the rotameter '28;

since it' avoids the necessity for renewing the adsorbent through the aspirator 29 is controlled bya needlegvalve or orifice; 33. -A second needle valve or orifice 132 is provided between the rotameter 28 and the inlet of the .aspirator 29 to controlfthe volume of oxidizing gases being drawn through the furnace ld,

The flow of the aspirated oxygen or ;air thronghthe pipe 10. This includes a conduitpipe means 85 Welded to the wall of standpipe 10 at an angle of about Gate valves 86 and 87 are "provided on pipe 85 to permit shutting oif the pipeSS when the sampling line 11 with its contained rod Alis withdrawn. In suchoperation, the packing gland .88 is released to permit the withdrawal of-the tube '11.. During this operation, flushing gas "is bled into the pipeIhS by meansof bleeds 89 and 90, :the

- intr.odnced gas having the .efieot .of clearing catalyst from the seats of gate valves 86 and 87 and of dislodging catalyst which 'mayhaveaccumulated between the sample tube 11 and conduit take-elf pipe85.

To replace the instrument, the procedure is reversed with an air blowing proceeding the introducing of the sample tube 11. If desired, the sample tube .11- may be" provided withindex marksto indicate the extent to which the inlet end of the sample tube 11 projects into the standpipe .10. 7 p p To prevent the entry .oflarger masses of solids into the'sampling tube 11, weprovide an internal sleeve -or collar 91 at the upper end of the sampling tube11 which acts :as a lump discriminator by reducing the annu 1 lar opening at the-inlet endof'the sample tube 11. The

inlet end of the sample tube 11 is rnitered so as .0 Pre-' sent a substantially vertical inlet face 92. Thisend,

however, projects inward into the solids how so as to sweep away any; larger particles which might become lodged about collar 91..

V The spent catalyst sample taken from the standpipe .10 issues from the catalyst delivery tube 11 onto the recessed periphery 35,0f the catalyst metering wheel 36.

The discharge end ofthedeliveq tube 11-is provided with a nozzle 40 through which arotating rod or spindle furnace 14 must be uniform to preclude variations :in

the partial pressure of the CO in the combustion ;gas.

Variations .in the partial pressure of cO resulting from sources other than thecarbon on the catalystwouldimpair the validity of the CO meter reading because it is a partialpressure measuring instrument. 7

7 Although ten to fifteentimes the required volume of the oxidizing gas is metered to the inlet of furnace 14 when commercial oxygen is used, only about eight times 'the theoretical based on,2 percent carbon on the catalyst is actually drawn through the furnace 14. The excess oxygen diffuses into the surrounding air and minimizes the possibility of dilution of the furnace intake with air. Further, when air' is the source of the oxidizing gas,and

.air is the reference gas'in 272', dilution is not a problem.

However, the use of air requires a higher furnace temperature for an equivalent amount of carbon bunn'ing Such lower temperature operation .is desir'able in some instances where the regenerated catalyst is periodically returned to the unit because temperatures in excess of about 1100 F.-ll50f F. may impair the life and activity ofsome cracking catalysts. However, in :commercial installations where the sample of catalyst 41 extends over the-length 0f the; delivery tube 11. The

rotating rod-41 has a tapered enlargement42 which is somewhat l-argerdhanfthe diameter of' the nozzle-40. The positionof the rotatingfr odand tapered section with. p respectyto the; nozzle 40 ,is adjusted as will be described below so that a flow-rate of catalystjs maintained someriphery .35.

A catalystdivertingishield 43 is fixed about the mine $0 and deflects the catalyst through a downward opening 44 onto ithemetering wheel 36. Q A drive-shaft45, which .is axially aligned :with rod 41 and maybe integral therewith, extends through ;a packing nut46 on the shield 43.

The excess catalyst-is scraped from the wheel 36 by'a.

levelinggs'craper 47 andzapair ofside scrapers 37 mounted ,on opposite sides ;of the casing 12. The leveling scraper '47' has TaQIOW ZPOItiOH 47a which rides on the periphery ofthe :wheel 36.1. The deflected catalyst falls into theexcess catalyst receiver 13 8 from which it may be returned periodically to the catalyst systemn 'As. the wheel'36 rotates, :the' measured (quantity of catalyst sample in the peripheral channel 35. ofwthe wheel .36.. separates 'therefrmrl :and :falls fthr'ough ithe'ichute. 39 into the furnace 14. Y The catalyst sample from the delivery tube 11 is discharged .throughlthe' adjustable annular orifice formed by nozzle '40 zandthetaperedsectionzfl of the rod 41." The rotating rod .41 :pireclndes plugging: of the discharge tube .11; We .hayefonndthat performance is more reliable with a delivery tube 11 sloped downwardly, for example atleast 30 with the horizontal and preferably 45 as shown in Figure 11.

Aeration of the catalyst by injecting steam or nitrogen or traces of ammonia gas through bleed 48 in the delivery tube 11 is desirable. In fact, some catalysts with poor flowing characteristics will not flow uniformly unless so aerated. The presence of arnmonia in the housing 34 also minimizes sticking of the catalyst to the metering wheel 36. The ammonia gas can be injected from a liquid ammonia source either alone or together with nitrogen and/or steam. Another source of ammonia gas found operable is the use of a wick in a container of aqueous ammonium hydroxide suspended within the metering assembly 12.

The slope of the tube 11 together with the rotating rod 41, collar 91, and aeration bleed 48 result in a uniform flow of the solids from the standpipe to the collection vessel 20. If desired, the temperature of the delivery tube 11 can be raised with an appropriate jacket heater (not shown) which improves the catalyst flow characteristics by preheating the catalyst.

The catalyst issues from the nozzle 4% continuously but at a variable flow rate. Such variability does not impair the performance of the catalyst sampling device provided that the flow rate is maintained above the minimum necessary to fill the recessed periphery 35 of the catalyst metering wheel 36. Any excess catalyst delivered by tube 11 onto the metering Wheel 36 is deflected by leveling scraper 47 and side scrapers 37 into the excess catalyst receiver 38 from which it can be returned manually or automatically to the catalyst standpipe or some other point in the catalyst system.

The metering wheel 36 rotating at a selected rate, for example .of about 22.5 revolutions per hour, carries the catalyst in the periphery 35 downward and discharges it into chute 39 leading into a sample collector or a furnace. The rate of rotation is dependent upon the dimensions of the recessed peripheral channel for any pre-selected catalyst flow rate. The wheel 36 illustrated may be about 4.5 inches in diameter with a channel 35 having a radius of about 0.125 inch. Other sizes and shapes of continuous peripheral channels 35 can be used, however.

With some types of solids there may be a tendency to stick in the channel 35 due to electrostatic forces. These forces tending to hold the catalyst particles together can be dissipated by providing a source of alpha particles within the periphery 35 of the metering wheel 36 and such dissipation assists subsequent removal of the catalyst by gravity flow into chute 39. The channel 35 can for example be plated or treated with an alpha particle emitting substance such as radium or some isotope of radium. This ionizes the surrounding air which promotes dissipation of the electrostatic charges of the catalyst particles which might otherwise cause agglomeration and sticking thereof within the channel.

In a typical installation, the inclined delivery tube 11 :comprises a section of standard stainless steel seamless tubing of about 0.270 inch I. D. provided with a nozzle .orifice h? threaded about the end thereof. The tube 11 {is supported in the assembly by means of block 51 arranged between the frame members 52 and 53 which are in turn fixed to the casing 34. A rod 41 is aligned with respect to the axis of the tube 11 and the orifice in nozzle 40 by means of a thrust bearing 49 mounted on adjustable thrust plate 55 and a contact bearing 46 carried by the catalyst diverting shield 43.

The rotating rod 41 has a tapered section 42 about 0.5 inch long which flares gradually over its length from about 0.125 inch to about 0.150 inch diameter. The tapered section 42 extends within the orifice 40, which may be about 0.1407 inch in diameter, to provide an annular opening through which the solids are discharged from the delivery tube 11. Screws 54 contact the thrust plate 55 which adjustably carries the thrust bearing 49.

6 A slide coupling 56 links the end of the drive shaft with the motor 58 supported by the frame members 52 and 53, the motor 58 being adapted to rotate the rod 41 through shaft 45 at about 180 revolutions per hour.

The wheel 36 is fixed by hub 59 to the axle 60 which is journaled in opposite sides of the casing 34 in bearings 61. A motor 62 mounted on the side of the casing 34 drives the axle 60 directly at about 22.5 R. P. H. It should be understood, however, that for a given metering rate the speed of rotation of the metering wheel is a function of the dimensions of the recessed periphery.

A wheel scraper 63 is pivotally mounted near its upper end on shaft 66 and held in contact with the periphery 35 of the metering wheel 36 by tension spring 67. The scraper 63 comprises an elongated hollow cylinder with a wall segment removed so as to provide a scraping edge 64 which conforms to the peripheral channel 35 in the metering wheel 36 to dislodge the catalyst and direct it downwardly through the lower end 65 of the hollow scraper 63.

Referring to Figures 1 and 4, oxygen from how meter 16 is injected through a plurality of orifices 7t and also through a tube 71 discharging into the catalyst chute 39. The major proportion of oxygen is introduced through the plurality of orifices 7% whereas the central tube 71 carries only suflicient oxygen to maintain an oxygen atmosphere within the catalyst inlet chute 39. If air is used as the oxidizing gas a simplified system can be provided by eliminating the flow meter 16 and drawing in air via and 71 or simply through the open housing 34. It is also found advantageous to space chute 39 with respect to coupling 63 so that an 0.125 inch air space separates the chute peripherally from the coupling.

The furnace is comprises in one embodiment a fourfoot section of 0.5 inch seamless, stainless steel tube 72 wound with a beaded Nichrome wire heater means distributed over its full length. A first heater unit 73 of about 1000 watts covers the 36-inch central section of the furnace tube whereas an inlet heater unit 74 of about watts and an outlet heater unit 7 5 of about 60 Watts covers the six-inch end sections 76 and 77. The entire unit or furnace 14 may be enclosed by a suitable heat insulation 83 as shown in the drawings.

Thermocouples 78, 79 and 80 are fixed to the outer furnace wall at the center of each of the three heater sections 73, 74 and 75. An exploratory thermowell 81 is provided for exploring temperatures along the entire length of the furnace tube 72 below the heater coil 73. The end heaters 7 and 75 may be controlled manually by means of variable transformer 82 and the associated conductors; whereas the central heater 73 is controlled by a miilivoltmeter on-olf type temperature controller 33. It is contemplated, however, that for most applications all the heaters can be sized and wound appropriately for direct operation in series from an volt A. C. source and controlled by controller 33.

The time required for the analyzer to respond to changes in deposit concentrations is dependent upon the solids residence time within the furnace, the solids transportation rate to the furnace, and the gas transportation rate to the product gas meter. The over-all time lag can be kept at a minimum by operating with a high furnace temperature which is permissible in most commercial applications. Use of such high furnace temperatures accelerates the rates of combustion, thereby lowering the minimum solids residence time within the furnace and permitting the use of a furnace of smaller volume. In any event the system described enables an operator to obtain prompt indications of significant variations in the components of the solids and enables the operator to take corrective measures. Thus to reduce a carbon deposit on catalysts, the feed-to-catalyst ratio in the reactor is reduced and/or the flow of catalyst from the regenerator can be cut back. Hence, the objects of our invention have been attained and we have provided thereto.

' a "novel: both for metering finely divided 'solids troma continuous flowing stream and -.a system for automatically'andicontinuou sly analyzing solids for deposits,

, This'applicationis' a continuation-in-part of our copending application Serial No. 234,638, filed June, '30, 1951 and entitled iContinuous Carbon-on Catalyst Analyzer, now U. s. 'Patent 2,753,246;

Although our invention has been described in terms of specific apparatus which is described in'considerable detail, it should be understood'that this is byway of 1 illustration only and that our invention is .not limited Alternative embodiments and operating tech- -niques' will become apparent to those skilled in the art in view of the description therein, and accordingly it is contemplated that modifications 'in both the methodand the apparatus of four invention can be made without 1 departing from the spirit of 'the described invention.

What we claim :is: t "l. A sampling and metering device for them solid materials comprising in combination a sampling tube discharging within a metering chamber, an aeration gas supply line entering said tube through'a wall thereof,

an adjustable and rotatable rod extending longitudinally within said-tube, a tapered section on said rod adjacent the outlet of said tube forming an adjustable annular orifice at the end of said tube, a driven metering wheel mounted to rotate in subjacent alignment with said orifice,

a continuousperipheral recess in said wheel adaptedtto I receive a' quantity of finely divided solids therein, a tubular scraper arranged to scrape the bottom of said wheel recess to discharge a metered amount of solids irom' said recess into said chamber, and gravity means for transferring the metered amount of solids from said chamber.

2. A sampling and metering device for fluent solid.

materials comprising in combination a solids delivery tube discharging within a metering chamber, an aeration gasinlet intermediate the ends of said tube, an adjustp i8 I V of said wheel tor discharging meteredamountof-soligls in alignment with the said wheelscrapen j 3. The device of claim 2-which includes a diverting shield about the discharge end of said tube directing from said recess, and a chute arranged'below said wheel solidsonto said metering: wheel. j r e 4. The samplingand metering device for fluent solid materials comprising in combination a solids delivery 7 tube discharging within a metering chamber, an adjuste and .said leveling scraper whereby excess solids :are ,col-

able and rotatable rod extending within and beyond the discharge end of said tube, a tapered section on said rod f adjacent the outlet of said delivery tube forming an annular orifice with the end of said tube, a metering wheel' mounted to rotate in subjacent alignment with said orifice, a continuous peripheral recess in' said wheel adapted to retain a quantity of finely divided solids therein, drive means for rotating said rod and said wheel, leveling :scraper means straddling the rotatable metering wheel,

recess-conforming wheel scraper arranged tangentially able and rota-table rod extending throughout the length of said'tu'be, said rod having a tapered section adjacent the outlet of said delivery'tube which forms an annular orifice with said tube, means for rotating said rod, a

metering wheel mounted to rotate belowsaid orifice in alignment therewith, a continuous peripheral recess in solids chute, a motor means for driving said wheel, and' an excess catalyst reservoir below said metering wheel lected separate from the solids discharged into said chute.

, 5. The apparatus of claim ,1 including a sleeve fixed within the inlet end of said sample tube restricting the. 'flow area between said rotated rodand tube. V

6. The apparatus of claim Lwhich includes a ,lcveiing scraper means extending transverse to the peripheral recess to level 'a metered amount of solids therein .and

wherein said tubular scraper forremoving the metered amount of solids is resiliently pivoted adjacent to :said metering wheel with its axis extending tangent thereto.

, References Cited in the file at this patent UNITED STATES :PATENTS 26,582 Van Golder Mar. 20, 1860 518,915 Clarkson' Apr. '24, 1894 1,092,741 Nagel Apr. 7, 1914 1,362,968 Stewart Dec. 21, 1920 Robison Nov, 10,1942 

1. A SAMPLING AND METERING DEVICE FOR FLUENT SOLID MATERIALS COMPRISING IN COMBINATION A SAMPLING TUBE DISCHARGING WITHIN A METERING CHAMBER, AN AERATION GAS SUPPLY LINE ENTERING SAID TUBE THROUGH A WALL THEREOF, AN ADJUSTABLE AND ROTATABLE ROD EXTENDING LONGITUDINALLY WITHIN SAID TUBE, A TAPERED SECTION ON SAID ROD ADJACENT THE OUTLET OF SAID TUBE FORMING AN ADJUSTABLE ANNULAR ORIFICE AT THE END OF SAID TUBE, A DRIVEN METERING WHEEL MOUNTED TO ROTATE IN SUBJACENT ALIGNMENT WITH SAID ORIFICE, A CONTINUOUS PERIPHERAL RECESS IN SAID WHEEL ADAPTED TO RECEIVE A QUANTITY OF FINELY DIVIDED SOLIDS THEREIN, A TUBULAR SCRAPER ARRANGED TO SCRAPE THE BOTTOM OF SAID WHEEL RECESS TO DISCHARGE A METERED AMOUNT OF SOLIDS FROM SAID RECESS INTO SAID CHAMBER, AND GRAVITY MEANS FOR TRANSFERRING THE METERING AMOUNT OF SOLIDS FROM SAID CHAMBER. 